CA2733080C - Process to prepare precipitated calcium carbonate implementing low charge acrylate a/o maleinate-containing polymer - Google Patents
Process to prepare precipitated calcium carbonate implementing low charge acrylate a/o maleinate-containing polymer Download PDFInfo
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- C—CHEMISTRY; METALLURGY
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- C01F11/00—Compounds of calcium, strontium, or barium
- C01F11/18—Carbonates
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F11/00—Compounds of calcium, strontium, or barium
- C01F11/18—Carbonates
- C01F11/182—Preparation of calcium carbonate by carbonation of aqueous solutions and characterised by an additive other than CaCO3-seeds
- C01F11/183—Preparation of calcium carbonate by carbonation of aqueous solutions and characterised by an additive other than CaCO3-seeds the additive being an organic compound
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- C09—DYES; PAINTS; POLISHES; NATURAL RESINS; ADHESIVES; COMPOSITIONS NOT OTHERWISE PROVIDED FOR; APPLICATIONS OF MATERIALS NOT OTHERWISE PROVIDED FOR
- C09C—TREATMENT OF INORGANIC MATERIALS, OTHER THAN FIBROUS FILLERS, TO ENHANCE THEIR PIGMENTING OR FILLING PROPERTIES ; PREPARATION OF CARBON BLACK ; PREPARATION OF INORGANIC MATERIALS WHICH ARE NO SINGLE CHEMICAL COMPOUNDS AND WHICH ARE MAINLY USED AS PIGMENTS OR FILLERS
- C09C1/00—Treatment of specific inorganic materials other than fibrous fillers; Preparation of carbon black
- C09C1/02—Compounds of alkaline earth metals or magnesium
- C09C1/021—Calcium carbonates
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- C—CHEMISTRY; METALLURGY
- C09—DYES; PAINTS; POLISHES; NATURAL RESINS; ADHESIVES; COMPOSITIONS NOT OTHERWISE PROVIDED FOR; APPLICATIONS OF MATERIALS NOT OTHERWISE PROVIDED FOR
- C09D—COATING COMPOSITIONS, e.g. PAINTS, VARNISHES OR LACQUERS; FILLING PASTES; CHEMICAL PAINT OR INK REMOVERS; INKS; CORRECTING FLUIDS; WOODSTAINS; PASTES OR SOLIDS FOR COLOURING OR PRINTING; USE OF MATERIALS THEREFOR
- C09D7/00—Features of coating compositions, not provided for in group C09D5/00; Processes for incorporating ingredients in coating compositions
- C09D7/40—Additives
- C09D7/60—Additives non-macromolecular
- C09D7/61—Additives non-macromolecular inorganic
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- D—TEXTILES; PAPER
- D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
- D21H—PULP COMPOSITIONS; PREPARATION THEREOF NOT COVERED BY SUBCLASSES D21C OR D21D; IMPREGNATING OR COATING OF PAPER; TREATMENT OF FINISHED PAPER NOT COVERED BY CLASS B31 OR SUBCLASS D21G; PAPER NOT OTHERWISE PROVIDED FOR
- D21H19/00—Coated paper; Coating material
- D21H19/66—Coatings characterised by a special visual effect, e.g. patterned, textured
- D21H19/68—Coatings characterised by a special visual effect, e.g. patterned, textured uneven, broken, discontinuous
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- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2004/00—Particle morphology
- C01P2004/01—Particle morphology depicted by an image
- C01P2004/03—Particle morphology depicted by an image obtained by SEM
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- C01P2004/00—Particle morphology
- C01P2004/10—Particle morphology extending in one dimension, e.g. needle-like
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- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2004/00—Particle morphology
- C01P2004/60—Particles characterised by their size
- C01P2004/61—Micrometer sized, i.e. from 1-100 micrometer
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- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2006/00—Physical properties of inorganic compounds
- C01P2006/12—Surface area
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- C01P2006/00—Physical properties of inorganic compounds
- C01P2006/22—Rheological behaviour as dispersion, e.g. viscosity, sedimentation stability
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08K—Use of inorganic or non-macromolecular organic substances as compounding ingredients
- C08K3/00—Use of inorganic substances as compounding ingredients
- C08K3/18—Oxygen-containing compounds, e.g. metal carbonyls
- C08K3/24—Acids; Salts thereof
- C08K3/26—Carbonates; Bicarbonates
-
- D—TEXTILES; PAPER
- D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
- D21H—PULP COMPOSITIONS; PREPARATION THEREOF NOT COVERED BY SUBCLASSES D21C OR D21D; IMPREGNATING OR COATING OF PAPER; TREATMENT OF FINISHED PAPER NOT COVERED BY CLASS B31 OR SUBCLASS D21G; PAPER NOT OTHERWISE PROVIDED FOR
- D21H17/00—Non-fibrous material added to the pulp, characterised by its constitution; Paper-impregnating material characterised by its constitution
- D21H17/20—Macromolecular organic compounds
- D21H17/33—Synthetic macromolecular compounds
- D21H17/34—Synthetic macromolecular compounds obtained by reactions only involving carbon-to-carbon unsaturated bonds
- D21H17/37—Polymers of unsaturated acids or derivatives thereof, e.g. polyacrylates
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- D—TEXTILES; PAPER
- D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
- D21H—PULP COMPOSITIONS; PREPARATION THEREOF NOT COVERED BY SUBCLASSES D21C OR D21D; IMPREGNATING OR COATING OF PAPER; TREATMENT OF FINISHED PAPER NOT COVERED BY CLASS B31 OR SUBCLASS D21G; PAPER NOT OTHERWISE PROVIDED FOR
- D21H17/00—Non-fibrous material added to the pulp, characterised by its constitution; Paper-impregnating material characterised by its constitution
- D21H17/63—Inorganic compounds
- D21H17/67—Water-insoluble compounds, e.g. fillers, pigments
- D21H17/675—Oxides, hydroxides or carbonates
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- D21H19/00—Coated paper; Coating material
- D21H19/36—Coatings with pigments
- D21H19/38—Coatings with pigments characterised by the pigments
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Abstract
Process to prepare a precipitated calcium carbonate (PCC) comprising the following steps: (i) providing CaO, which is optionally partially or fully slaked (hereafter "calcium source"); (~) providing a CO2-comprising gas; (~) contacting said calcium source of step (i) and said CO2-comprising gas of step (ii) in an aqueous environment in a reactor, in one or more steps; (iv) obtaining a PCC-comprising suspension; (v) optionally concentrating said PCC-comprising suspension of step (iv); (vi) optionally adding dispersing additives to the suspension of step (iv) and/or (v); (vii) optionally grinding the product of step iv, v or vi.
Description
2 PCT/IB2009/006431 PROCESS TO PREPARE PRECIPITATED CALCIUM CARBONATE
IMPLEMENTING LOW CHARGE ACRYLATE a/o MALEINATE
-CONTAINING POLYMER
Synthetic calcium carbonate, referred to hereafter as precipitated calcium carbonate (PCC), is a known filler and coating pigment, particularly implemented in paper applications. It is obtained by hydration of calcium oxide (CaO), or "burnt lime", forming a suspension of calcium hydroxide (Ca(OH)2); this hydration step is also referred to as a step of "slaking lime". The obtained calcium hydroxide is thereafter precipitated by bubbling CO2 gas through the suspension, to form PCC.
Depending on the precipitation conditions, various polymorphs of PCC may be obtained, including aragonitic and scalenohedral polymorphs. The nature of the polymorph is generally determined based on analysis of scanning electron microscope (SEM) images of the product, aragonite crystal being generally needle-shaped as opposed to the ovoid form of scalenohedral products.
The skilled man refers to the PCC production capacity in terms of the weight of PCC
produced relative to both the carbonation time and the weight of the final PCC
suspension. Increasing this production capacity, namely by decreasing the carbonation time without overly increasing the final PCC suspension weight through addition of water to limit suspension viscosity, represents a goal of significant economical interest.
For the purpose of the present invention, carbonation time is the time from the start of introduction of COz-containing gas to a calcium source in suspension to reaching a minimum suspension conductivity.
A number of studies have addressed decreasing carbonation time, including WO
07365, in which this is said to be achieved by reducing the carbonation reactor pressure, through which COz gas is bubbled, to below atmospheric pressure. However, this approach implies costly modifications to the PCC production equipment.
Additives are also known to be implemented during the PCC production process in order to reduce carbonation time. According to Change of formation yield and characterization of PCC particle synthesized with impurity ions by carbonation process >>
CONFIRMATION COPY
(Materials Science Forum, 510-511, March 2006, pp. 1026-1029), this is achieved by addition of ions, such as aluminium, iron and magnesium; however, the crystallographic structure, or polymorph, of the resulting PCC differs relative to the PCC that would be obtained via a process excluding these ions.
In << Morphological characteristics and aggregation of calcite crystals obtained by bubbling CO2 through Ca(OH)2 suspension in the presence of additives >> (Powder Technology, 130, 2003, pp. 307-315), the addition of citric acid, sucrose or calcium lignosulfonate to a suspension of slaked lime prior to the carbonation process is remarked to significantly extend carbonation time, whereas polyethylene glycol (of molecular weight 300 g/mol) is proposed to decrease this time. However, as shown in the Examples section herebelow, processes implementing polyethylene glycols fail to provide the improvement in PCC
production capacity provided by the process of the present invention.
Lastly, WO 2005 / 000742 and WO 2004 / 106236 disclose a PCC production process in which a polyacrylate and polyphosphate are added prior to completion of the carbonation reaction. These documents fail to refer to any influence these additives might have on carbonation time. Indeed, as shown in the Examples herebelow, PCC production processes implementing such simple polyacrylates do not allow the same, advantageous improvement in PCC production capacity as do the processes of the present invention.
Additionally, these documents clearly suggest that the crystallographic PCC
structures obtained in the presence of the mentioned additives differ from that obtained in their absence.
As such, the skilled man has no leading line suggesting a process to solve the problem of improving the PCC production capacity, namely by reducing carbonation time, subject to the following constraints:
- to identify a chemical additive allowing the carbonation time to be reduced without requiring extensive and often costly modifications to be made to his production equipment;
- to identify a chemical additive that does not change the crystallographic structure of the obtained PCC relative to the structure obtained by the same process but in absence of said additive;
IMPLEMENTING LOW CHARGE ACRYLATE a/o MALEINATE
-CONTAINING POLYMER
Synthetic calcium carbonate, referred to hereafter as precipitated calcium carbonate (PCC), is a known filler and coating pigment, particularly implemented in paper applications. It is obtained by hydration of calcium oxide (CaO), or "burnt lime", forming a suspension of calcium hydroxide (Ca(OH)2); this hydration step is also referred to as a step of "slaking lime". The obtained calcium hydroxide is thereafter precipitated by bubbling CO2 gas through the suspension, to form PCC.
Depending on the precipitation conditions, various polymorphs of PCC may be obtained, including aragonitic and scalenohedral polymorphs. The nature of the polymorph is generally determined based on analysis of scanning electron microscope (SEM) images of the product, aragonite crystal being generally needle-shaped as opposed to the ovoid form of scalenohedral products.
The skilled man refers to the PCC production capacity in terms of the weight of PCC
produced relative to both the carbonation time and the weight of the final PCC
suspension. Increasing this production capacity, namely by decreasing the carbonation time without overly increasing the final PCC suspension weight through addition of water to limit suspension viscosity, represents a goal of significant economical interest.
For the purpose of the present invention, carbonation time is the time from the start of introduction of COz-containing gas to a calcium source in suspension to reaching a minimum suspension conductivity.
A number of studies have addressed decreasing carbonation time, including WO
07365, in which this is said to be achieved by reducing the carbonation reactor pressure, through which COz gas is bubbled, to below atmospheric pressure. However, this approach implies costly modifications to the PCC production equipment.
Additives are also known to be implemented during the PCC production process in order to reduce carbonation time. According to Change of formation yield and characterization of PCC particle synthesized with impurity ions by carbonation process >>
CONFIRMATION COPY
(Materials Science Forum, 510-511, March 2006, pp. 1026-1029), this is achieved by addition of ions, such as aluminium, iron and magnesium; however, the crystallographic structure, or polymorph, of the resulting PCC differs relative to the PCC that would be obtained via a process excluding these ions.
In << Morphological characteristics and aggregation of calcite crystals obtained by bubbling CO2 through Ca(OH)2 suspension in the presence of additives >> (Powder Technology, 130, 2003, pp. 307-315), the addition of citric acid, sucrose or calcium lignosulfonate to a suspension of slaked lime prior to the carbonation process is remarked to significantly extend carbonation time, whereas polyethylene glycol (of molecular weight 300 g/mol) is proposed to decrease this time. However, as shown in the Examples section herebelow, processes implementing polyethylene glycols fail to provide the improvement in PCC
production capacity provided by the process of the present invention.
Lastly, WO 2005 / 000742 and WO 2004 / 106236 disclose a PCC production process in which a polyacrylate and polyphosphate are added prior to completion of the carbonation reaction. These documents fail to refer to any influence these additives might have on carbonation time. Indeed, as shown in the Examples herebelow, PCC production processes implementing such simple polyacrylates do not allow the same, advantageous improvement in PCC production capacity as do the processes of the present invention.
Additionally, these documents clearly suggest that the crystallographic PCC
structures obtained in the presence of the mentioned additives differ from that obtained in their absence.
As such, the skilled man has no leading line suggesting a process to solve the problem of improving the PCC production capacity, namely by reducing carbonation time, subject to the following constraints:
- to identify a chemical additive allowing the carbonation time to be reduced without requiring extensive and often costly modifications to be made to his production equipment;
- to identify a chemical additive that does not change the crystallographic structure of the obtained PCC relative to the structure obtained by the same process but in absence of said additive;
3 - to identify a chemical additive that does not lead to overly high PCC
suspension viscosities, requiring the addition of significant amounts of dilution water, said dilution water being a limiting factor in the PCC production rate;
- to identify a chemical additive that leads to an aqueous suspension featuring a high PCC solids content, the solids being among the factors contributing to the overall production costs of the PCC material.
In response to this multi-faceted technical problem, the Applicant has surprisingly identified a process to prepare a precipitated calcium carbonate (PCC) comprising the following steps:
(i) providing CaO, which is optionally partially or fully slaked (hereafter "calcium source");
(ii) providing a C02-comprising gas;
(iii) contacting said calcium source of step (i) and said C02-comprising gas of step (ii) in an aqueous environment in a reactor, in one or more steps;
(iv) obtaining a PCC-comprising suspension;
(v) optionally concentrating said PCC-comprising suspension of step (iv);
(vi) optionally adding dispersing additives to the suspension of step (iv) and/or (v);
(vii) optionally grinding the product of step iv, v or vi;
characterised in that:
- at least one polymer resulting from the polymerisation of the following monomers, where such monomers are present in said polymer in the following % monomer units relative to the total monomer units forming said polymer, is present during step (iii):
a) from 10 % to 99 %, preferably from 50 % to 98 %, more preferably from 80 %
to 97 %, and even more preferably from 85 % to 95 %, of at least one vinyl group-comprising monomer not comprising Formula (I), b) from 1% to 90%, preferably from 2 % to 50 %, more preferably from 3 % to 20 %, and even more preferably from 5 % to 15 %, of at least one vinyl group-comprising monomer having at least one substituent comprising Formula (I) :
Ri R2 R=
/R n 0
suspension viscosities, requiring the addition of significant amounts of dilution water, said dilution water being a limiting factor in the PCC production rate;
- to identify a chemical additive that leads to an aqueous suspension featuring a high PCC solids content, the solids being among the factors contributing to the overall production costs of the PCC material.
In response to this multi-faceted technical problem, the Applicant has surprisingly identified a process to prepare a precipitated calcium carbonate (PCC) comprising the following steps:
(i) providing CaO, which is optionally partially or fully slaked (hereafter "calcium source");
(ii) providing a C02-comprising gas;
(iii) contacting said calcium source of step (i) and said C02-comprising gas of step (ii) in an aqueous environment in a reactor, in one or more steps;
(iv) obtaining a PCC-comprising suspension;
(v) optionally concentrating said PCC-comprising suspension of step (iv);
(vi) optionally adding dispersing additives to the suspension of step (iv) and/or (v);
(vii) optionally grinding the product of step iv, v or vi;
characterised in that:
- at least one polymer resulting from the polymerisation of the following monomers, where such monomers are present in said polymer in the following % monomer units relative to the total monomer units forming said polymer, is present during step (iii):
a) from 10 % to 99 %, preferably from 50 % to 98 %, more preferably from 80 %
to 97 %, and even more preferably from 85 % to 95 %, of at least one vinyl group-comprising monomer not comprising Formula (I), b) from 1% to 90%, preferably from 2 % to 50 %, more preferably from 3 % to 20 %, and even more preferably from 5 % to 15 %, of at least one vinyl group-comprising monomer having at least one substituent comprising Formula (I) :
Ri R2 R=
/R n 0
4 Formula (I) wherein :
- m, n, p and q are whole numbers having a value of less than 150, and at least one of m, n, p and' q has a value of greater than 0, such that 25 <_ (m+n+p)q _< 150, and preferably such that 50 (m+n+p)q < 150;
- R represents a functional linking group selected from ethers, esters or amides, - R, and R2 are the same or different, and represent hydrogen or alkyl groups having 1 to 4 carbon atoms, - R' represents hydrogen or a hydrocarbon radical having 1 to 40, preferably 1 to 3, carbon atoms, R' being even more preferably a methyl radical or hydrogen, the sum of the monomer unit percentages of monomers a) and b) being equal to 100 %.
The Applicant would like to mention FR 2,911,147, which discloses the use of similar polymers for the dispersing of metal oxides and hydroxides; in this document, no mention is made of the use of such polymers in a process to produce PCC having a reduced carbonation time subject to the above-mentioned requirements of the skilled man. To the contrary, the proposed increase in calcium oxide hydration time in FR
2,911,147 would rather drive the skilled man not to implement such polymers in view of his goal to develop an efficient PCC production process.
Preferred embodiments relative to the polymer:
In a preferred embodiment, monomer(s) (a) are selected from among anionic monomers, such as acrylic, methacrylic or maleic acid, cationic monomers such as acrylamide,
- m, n, p and q are whole numbers having a value of less than 150, and at least one of m, n, p and' q has a value of greater than 0, such that 25 <_ (m+n+p)q _< 150, and preferably such that 50 (m+n+p)q < 150;
- R represents a functional linking group selected from ethers, esters or amides, - R, and R2 are the same or different, and represent hydrogen or alkyl groups having 1 to 4 carbon atoms, - R' represents hydrogen or a hydrocarbon radical having 1 to 40, preferably 1 to 3, carbon atoms, R' being even more preferably a methyl radical or hydrogen, the sum of the monomer unit percentages of monomers a) and b) being equal to 100 %.
The Applicant would like to mention FR 2,911,147, which discloses the use of similar polymers for the dispersing of metal oxides and hydroxides; in this document, no mention is made of the use of such polymers in a process to produce PCC having a reduced carbonation time subject to the above-mentioned requirements of the skilled man. To the contrary, the proposed increase in calcium oxide hydration time in FR
2,911,147 would rather drive the skilled man not to implement such polymers in view of his goal to develop an efficient PCC production process.
Preferred embodiments relative to the polymer:
In a preferred embodiment, monomer(s) (a) are selected from among anionic monomers, such as acrylic, methacrylic or maleic acid, cationic monomers such as acrylamide,
5 methacrylamide, neutral monomers such as acrylic, methacrylic or maleic acid esters, or mixtures thereof.
In a preferred embodiment, said monomer(s) (a) are a mixture of anionic and neutral monomer(s). In such a case, it is further preferred that the monomer unit ratio of anionic monomers:neutral monomers be from 50:50 to 2:1, more preferably of 8:1 to 12:1, and most preferably of 10:1.
In a preferred embodiment, said monomer(s) (a) are a mixture of anionic and neutral monomer(s) selected from among acrylic and/or methacrylic acids and esters thereof.
In the case where cationic monomers are selected, it is preferred that these be selected from among cationic (meth)acrylic esters, and preferably from among chloride and/or sulfate salts of one or more of the following: [2-(methacryloyloxy)ethyl]trimethyl ammonium, [3-acrylamido)propyl]trimethylammonium, dimethyl diallyl ammonium, [3-(methacrylamido)propyl]trimethylanunonium.
As regards monomer(s) (b), these may additionally feature substituents not comprising Formula (I) selected from one or more of the following functional groups:
alkyl, aryl, allcyl ester, hydrogen, alkyl amide, carboxyl and allyl, and preferably features at least one methyl substituent. In a preferred embodiment, monomer(s) (b) feature a methyl group in trans- position relative to the substituent comprising Formula (I) in which said functional group linking is an ester.
In another embodiment, monomer(s) (b) have at least one substituent consisting of Formula (I).
It may further be of interest that said polymer features an intrinsic viscosity of less than or equal to 100 ml/g, as determined by the method described in "Outlines of macromolecular chemistry" volume III (Vollmert Verlag, Karlsruhe 1985), implementing a solution of
In a preferred embodiment, said monomer(s) (a) are a mixture of anionic and neutral monomer(s). In such a case, it is further preferred that the monomer unit ratio of anionic monomers:neutral monomers be from 50:50 to 2:1, more preferably of 8:1 to 12:1, and most preferably of 10:1.
In a preferred embodiment, said monomer(s) (a) are a mixture of anionic and neutral monomer(s) selected from among acrylic and/or methacrylic acids and esters thereof.
In the case where cationic monomers are selected, it is preferred that these be selected from among cationic (meth)acrylic esters, and preferably from among chloride and/or sulfate salts of one or more of the following: [2-(methacryloyloxy)ethyl]trimethyl ammonium, [3-acrylamido)propyl]trimethylammonium, dimethyl diallyl ammonium, [3-(methacrylamido)propyl]trimethylanunonium.
As regards monomer(s) (b), these may additionally feature substituents not comprising Formula (I) selected from one or more of the following functional groups:
alkyl, aryl, allcyl ester, hydrogen, alkyl amide, carboxyl and allyl, and preferably features at least one methyl substituent. In a preferred embodiment, monomer(s) (b) feature a methyl group in trans- position relative to the substituent comprising Formula (I) in which said functional group linking is an ester.
In another embodiment, monomer(s) (b) have at least one substituent consisting of Formula (I).
It may further be of interest that said polymer features an intrinsic viscosity of less than or equal to 100 ml/g, as determined by the method described in "Outlines of macromolecular chemistry" volume III (Vollmert Verlag, Karlsruhe 1985), implementing a solution of
6 double-distilled water and a capillary tube according to DIN 53101/Oa (having a constant of 0.005 and a diameter of 0.53 mm).
Any dissociated acid groups in said polymer may be partially or fully neutralised by one or more neutralisation agents having a monovalent or polyvalent cation, said neutralisation agents being preferably selected from among ammonia or from among calcium, sodium, magnesium, potassium or lithium hydroxides or oxides, or from among primary, secondary or tertiary aliphatic and/or cyclic amines, and preferably from among stearyl amine, mono-, di- or triethanoamines, cyclohexylamine, methylcyclohexylamine, aminomethylpropanol, morpholine, said neutralisation agent being preferably sodium hydroxide.
Before or after any neutralisation reaction, said polymer may be treated and separated into multiple phases, by static or dynamic processes, by one or more polar solvents, said solvents being preferably selected from among water, methanol, ethanol, propanol, isopropanol, butanol, acetone, tetrahydrofuran, or mixtures thereof.
The polymer may be obtained via a process of radical polymerisation in solution, in direct or inverse emulsion, in suspension or by precipitation in solvents, in the presence of catalytic systems or transfer agents, or via a controlled radical polymerisation, preferably controlled by nitroxides (NMP) or by cobaloximes, or by Atom Transfer Radical Polymerisation (ATRP), by sulphur-derivative controlled radical polymerisation, selected from among carbamates, dithioesters or trithiocarbonates (Reversible Addition-Fragmentation chain Transfer or RAFT) or xanthates.
Preferred embodiments relative to the polymer addition amount and moment of addition:
It is preferred that the polymer is added to the process in amount totalling 0.01 to 0.5, preferably 0.05 to 0.2 % by dry weight relative to the dry weight of PCC
obtained in step (iv).
Said polymer may be fractionated in doses added over time prior to and/or during step (iii)=
Moreover, said polymer may be added during more than one of steps (i), (ii) and (iii).
Any dissociated acid groups in said polymer may be partially or fully neutralised by one or more neutralisation agents having a monovalent or polyvalent cation, said neutralisation agents being preferably selected from among ammonia or from among calcium, sodium, magnesium, potassium or lithium hydroxides or oxides, or from among primary, secondary or tertiary aliphatic and/or cyclic amines, and preferably from among stearyl amine, mono-, di- or triethanoamines, cyclohexylamine, methylcyclohexylamine, aminomethylpropanol, morpholine, said neutralisation agent being preferably sodium hydroxide.
Before or after any neutralisation reaction, said polymer may be treated and separated into multiple phases, by static or dynamic processes, by one or more polar solvents, said solvents being preferably selected from among water, methanol, ethanol, propanol, isopropanol, butanol, acetone, tetrahydrofuran, or mixtures thereof.
The polymer may be obtained via a process of radical polymerisation in solution, in direct or inverse emulsion, in suspension or by precipitation in solvents, in the presence of catalytic systems or transfer agents, or via a controlled radical polymerisation, preferably controlled by nitroxides (NMP) or by cobaloximes, or by Atom Transfer Radical Polymerisation (ATRP), by sulphur-derivative controlled radical polymerisation, selected from among carbamates, dithioesters or trithiocarbonates (Reversible Addition-Fragmentation chain Transfer or RAFT) or xanthates.
Preferred embodiments relative to the polymer addition amount and moment of addition:
It is preferred that the polymer is added to the process in amount totalling 0.01 to 0.5, preferably 0.05 to 0.2 % by dry weight relative to the dry weight of PCC
obtained in step (iv).
Said polymer may be fractionated in doses added over time prior to and/or during step (iii)=
Moreover, said polymer may be added during more than one of steps (i), (ii) and (iii).
7 It is preferred that 20, preferably 50, more preferably 80, and most preferably 100 % by weight of the polymer be added prior to reaching an aqueous environment maximum viscosity during step (iii).
It may also be preferred that 20, preferably 50, more preferably 80, and most preferably 100 % by weight of the polymer is added prior to reaching an aqueous environment conductivity drop associated with a conductivity curve inflection point slope of more than 45 during step (iii).
It may also be preferred that 20, preferably 50, more preferably 80, and most preferably 100 % by weight of the polymer is added prior to reaching a pH value of less than 7.2 during step (iii).
In one embodiment, 20, preferably 50, more preferably 80, and most preferably 100 % by weight of the polymer is added prior to step (iii).
It is possible that said CaO of step (i) is partially or fully slaked by addition of slaking water to form a slaked lime suspension prior to step (iii). In such a case, 20, preferably 50, more preferably 80, and most preferably 100 % by weight of the polymer may be added to said slaking water.
In another embodiment, 20, preferably 50, more preferably 80, and most preferably 100 %
by weight of the polymer is added to the already slaked lime suspension prior to step (iii).
Preferred embodiments relative to the step (iii):
As regards step (iii), C02-comprising gas may be bubbled through the aqueous environment until this environment has a pH drop to 7.5, and preferably to 7.2.
C02-comprising gas may be bubbled through the aqueous environment until this environment has a conductivity drop. As shown in the Examples herebelow, to ensure a maximum of PCC is formed, it may also be of interest to continue bubbling the comprising gas through the slurry for some time following this conductivity drop.
It may also be preferred that 20, preferably 50, more preferably 80, and most preferably 100 % by weight of the polymer is added prior to reaching an aqueous environment conductivity drop associated with a conductivity curve inflection point slope of more than 45 during step (iii).
It may also be preferred that 20, preferably 50, more preferably 80, and most preferably 100 % by weight of the polymer is added prior to reaching a pH value of less than 7.2 during step (iii).
In one embodiment, 20, preferably 50, more preferably 80, and most preferably 100 % by weight of the polymer is added prior to step (iii).
It is possible that said CaO of step (i) is partially or fully slaked by addition of slaking water to form a slaked lime suspension prior to step (iii). In such a case, 20, preferably 50, more preferably 80, and most preferably 100 % by weight of the polymer may be added to said slaking water.
In another embodiment, 20, preferably 50, more preferably 80, and most preferably 100 %
by weight of the polymer is added to the already slaked lime suspension prior to step (iii).
Preferred embodiments relative to the step (iii):
As regards step (iii), C02-comprising gas may be bubbled through the aqueous environment until this environment has a pH drop to 7.5, and preferably to 7.2.
C02-comprising gas may be bubbled through the aqueous environment until this environment has a conductivity drop. As shown in the Examples herebelow, to ensure a maximum of PCC is formed, it may also be of interest to continue bubbling the comprising gas through the slurry for some time following this conductivity drop.
8 It is preferred that this C02-comprising gas be provided to the reactor at an overpressure of at least 0.1, preferably of at least 0.2, more preferably of at least 0.3, even more preferably of at least 0.4 and most preferably of at least 0.6 bar relative to the pressure in said reactor.
The pressure in the reactor is generally between 50 mbar and 25 bar, and preferably is 1 bar.
The volume fraction of CO2 in said C02-comprising gas is generally greater than 4 %. As shown in the Examples, the skilled man may indeed even wish to vary the CO2 content of this gas over the carbonation time.
The rate of C02-comprising gas introduction may also be adapted by the skilled man. In general, it is greater than or equal to 100 m3/h.
The CO2 gas of said C02-comprising gas may be "fresh" CO2 according to FR 2 The CO2 gas might even be obtained from dry ice.
Preferred embodiments relative to other aspects of the process:
The skilled man will know to adapt his process conditions (such as temperature, use of seeds or additional additives prior to and/or during step (iii)) to the quality of his starting materials according to the PCC polymorph he intends to produce. The skilled man will know, among other parameters, to adapt his reactor volume and the solids content of Ca(OH)2 suspension, the CO2 partial pressure in feed gas, gas feed rate and CO2 yield (reactor efficiency) according to the product he desires.
He might grind CaO and/or the Ca(OH)2 suspension, optionally before and/or during the addition of the polymer.
He might elect to add dry CaO to already slaked lime prior to carbonation in order to increase the solids of the Ca(OH)2 suspension.
He may run the process of the present invention as a continuous or batch process.
The pressure in the reactor is generally between 50 mbar and 25 bar, and preferably is 1 bar.
The volume fraction of CO2 in said C02-comprising gas is generally greater than 4 %. As shown in the Examples, the skilled man may indeed even wish to vary the CO2 content of this gas over the carbonation time.
The rate of C02-comprising gas introduction may also be adapted by the skilled man. In general, it is greater than or equal to 100 m3/h.
The CO2 gas of said C02-comprising gas may be "fresh" CO2 according to FR 2 The CO2 gas might even be obtained from dry ice.
Preferred embodiments relative to other aspects of the process:
The skilled man will know to adapt his process conditions (such as temperature, use of seeds or additional additives prior to and/or during step (iii)) to the quality of his starting materials according to the PCC polymorph he intends to produce. The skilled man will know, among other parameters, to adapt his reactor volume and the solids content of Ca(OH)2 suspension, the CO2 partial pressure in feed gas, gas feed rate and CO2 yield (reactor efficiency) according to the product he desires.
He might grind CaO and/or the Ca(OH)2 suspension, optionally before and/or during the addition of the polymer.
He might elect to add dry CaO to already slaked lime prior to carbonation in order to increase the solids of the Ca(OH)2 suspension.
He may run the process of the present invention as a continuous or batch process.
9 He may adapt the aqueous environment agitation rate, though this generally lies between 200 to 300 rpm during step (iii).
Following the obtention of the PCC-comprising suspension in step (iv), he may wish to concentrate this suspension by mechanical and/or thermal concentration. During such a concentration, it may be advantageous to add dispersing additives, such as common polyacrylates.
It is of note that should additional polymer according to the present invention be implemented as a dispersant during steps (v) and (vi), less must be added than when concentrating a PCC-comprising suspension not obtained by the present invention.
Said PCC of step (iv) may also be dried.
Product-by-process The present invention also lies in the aqueous suspension from the inventive process.
The present invention also lies in a dry product obtained by drying the aqueous suspension from the inventive process.
As regards this dry product, it generally features the same or less residual calcium hydroxide as a product obtained by the same process but in the absence of said polymer, the residual lime content being determined by XRD analysis. Indeed, it is among the advantages of the present invention that the degree of conversion of calcium hydroxide to PCC is not negatively affected.
Moreover, this dry product may contain less than 6 %, and preferably less than 3 %, by weight relative to the weight of the total product weight, of residual calcium hydroxide.
Use of the product-by-process The PCC-comprising suspension or dry product obtained following the process of the 5 present invention finds applications in paper, paint or plastic, and especially in paper or plastic.
EXAMPLES
Example 1 In the Tests below, PCC was synthesised by bubbling a C02-comprising gas through a suspension of calcium hydroxide.
Additives according to the prior art and according to the process of the invention were implemented. The following prior art additives were used:
- PAA is a sodium polyacrylate with a molecular weight of about 10 500 g/mol - PEG is a polyethylene glycol with a molecular weight of about 600 g/mol The following additive according to the process of the invention was used:
- Polymer P is a polymer resulting from the polymerisation of the following monomers (expressed in % monomer units of each constituent):
- monomer a) 79,8 % of methacrylic acid and 9,0 % of ethyl acrylate - monomer b) 11,2 % of a monomer featuring a vinyl group on which:
- a first substituent consists of Formula (I), wherein:
R = ester function;
R' = methyl group;
m = 0;
p0;
n = 45;
q= 1;
- a second substituent consists of a methyl group;
- the first and second substituents above are in trans-position relative to one another.
The efficiency of the PCC production process was determined according to the weight of PCC produced (in kg) relative to both carbonation time (in hours) and final PCC
suspension weight (in kg).
The obtained precipitated calcium carbonate polymorph was determined by visual analysis of the SEM images of the product.
The particle size characteristics of the obtained PCC (median diameter (dso), where the value dx represents the diameter relative to which X % by weight of the particles have a diameter less than dx) was determined based on measurements made using SedigraphTM
5100 instrumentation from MICROMERITICSTM.
The specific surface area (in m2/g) of the obtained PCC was determined using the BET
method, according to ISO 9277:1995.
The BrookfieldTM viscosity of the final PCC suspension was measured at 25 C
under 100 rpm ( i2).
Residual lime content in the obtained PCC was determined by XRD analysis.
Test 1 (Reference process for the production of scalenohedral PCC) 200 kg of calcium oxide (origin: Austria) were added to 1 700 litres of 40 C-tap water in a stirred reactor; the reactor contents were mixed under continuous stirring for 30 minutes. The resulting suspension of calcium hydroxide was diluted with water to obtain a suspension featuring a dry weight of calcium hydroxide as listed in Table 1.
1 750 litres of this calcium hydroxide suspension was then brought to a temperature of 50 C and directed into a 1 800 litre cylindrical stainless steel reactor equipped with an agitator and probes monitoring the pH and conductivity of the suspension.
A gas of 20-30 % by volume of CO2 in air was then bubbled upwards through the suspension at a rate of 200 m3/h under a suspension agitation of between 200 and 300 rpm. Overpressure in gas feed was 150-200 mbar, corresponding to hydrostatic pressure of Ca(OH)2 suspension in the reactor.
During carbonation, the temperature of the suspension was not controlled and allowed to rise due to the heat generated in the exothermic precipitation reaction.
After conductivity reached a minimum, gassing was continued for another 4 minutes and then stopped. The final product had a residual lime content of less than 6 %
by weight relative to the weight of the final PCC product.
Carbonation time, representing the time elapsed between the start of gas introduction and reaching a conductivity minimum, and other product and process conditions, are given in Table 1.
Test 2 (Prior art process for the production of scalenohedral PCC) This test was run under the same conditions as Test 1, according to the conditions listed in Table 1, with the addition of PAA to the Ca(OH)2 suspension prior to carbonation in an amount listed in Table 1.
Results are given in Table 1.
Test 3 (Process according to the invention for the production of scalenohedral PCC) This test was run under the same conditions as Test 1, according to the conditions listed in Table 1, with the addition of Polymer P to the Ca(OH)2 suspension prior to carbonation in an amount listed in Table 1.
The final PCC product had a residual lime content of less than 6 % by weight.
Other results are given in Table 1.
Test 4 (Reference process for the production of aragonitic PCC) 160 kg of calcium oxide (origin: USA) were added to 1 300 litres of 50 C-tap water in a stirred reactor; the reactor contents were mixed under continuous stirring for 30 minutes.
The resulting suspension of calcium hydroxide was diluted with water to obtain a suspension featuring a dry weight of calcium hydroxide as listed in Table 1.
1 250 litres of this calcium hydroxide suspension was then brought to a temperature of 60 C and directed into a 1 800 litre cylindrical stainless steel reactor equipped with an agitator and probes monitoring the pH and conductivity of the suspension as well as the CO2 content of the exhaust gas.
Before start of carbonation, aragonite structure-promoting seed was added to the calcium hydroxide suspension.
A gas of 4-8 % by volume of CO2 in air was then bubbled upwards through the suspension at a rate of 100 m3/h under a suspension agitation of 200 to 300 rpm during 15 minutes, calculated from start of introduction of said gas. Thereafter, the CO2 volume fraction in the gas was augmented to 20-30 % under the same conditions until the end of the carbonation. Overpressure in gas feed was 100-150 mbar, corresponding to hydrostatic pressure of Ca(OH)2 suspension in the reactor.
When the C02-content in the exhaust gas exceeded 6 % by volume, hot dilution water, in an amount listed in Table 1, was added continuously into the reactor to obtain the viscosity listed in Table 1.
During carbonation, the temperature of the suspension was not controlled and allowed to rise due to the heat generated in the exothermic precipitation reaction.
After conductivity reached a minimum, gassing was continued for another 4 minutes and then stopped. The final product had a residual lime content of less than 6 %
by weight relative to the weight of the final PCC product.
5 Carbonation time, representing the time elapsed between the start of gas introduction and reaching a conductivity minimum, and other product and process conditions are given in Table 1.
Test 5 (Process according to the invention for the production of aragonitic PCC) This test was run under the same conditions as Test 4, according to the conditions listed in Table 1, with the addition of Polymer P to the water subsequently added to calcium oxide to form the calcium hydroxide suspension, in an amount listed in Table 1.
The final PCC product had a residual lime content of less than 6 % by weight.
Other results are given in Table 1.
Test 6 (Process according to the invention for the production of aragonitic PCC) This test was run under the same conditions as Test 4, according to the conditions listed in Table 1, with the addition of Polymer P to the calcium hydroxide suspension prior to commencing carbonation, in an amount listed in Table 1.
The final PCC product had a residual lime content of less than 6 % by weight.
Other results are given in Table 1.
Test 7 (Process according to the invention for the production of aragonitic PCC) This test was run under the same conditions as Test 4, according to the conditions listed in Table 1, with the addition of Polymer P to the calcium hydroxide suspension prior to commencing carbonation, in an amount listed in Table 1.
The final PCC product had a residual lime content of less than 6 % by weight.
Other results are given in Table 1.
Test 8 (Process according to the invention for the production of aragonitic PCC) This test was run under the same conditions as Test 4, according to the conditions listed in Table 1, with the addition of Polymer P to the calcium hydroxide suspension prior to commencing carbonation, in an amount listed in Table 1.
The final PCC product had a residual lime content of less than 6 % by weight.
Other results are given in Table 1.
Test 9 (Reference process for the production of aragonitic PCC) 160 kg of calcium oxide (origin: Austria) were added to 1 300 litres of 50 C-tap water in a stirred reactor; the reactor contents were mixed under continuous stirring for 30 minutes. The resulting suspension of calcium hydroxide was diluted with water to obtain a suspension featuring a dry weight of calcium hydroxide as listed in Table 1.
1 250 litres of this calcium hydroxide suspension was then brought to a temperature of 60 C and directed into a 1 800 litre cylindrical stainless steel reactor equipped with an agitator and probes monitoring the pH and conductivity of the suspension as well as the CO2 content of the exhaust gas.
Before the start of carbonation, aragonite structure-promoting seed was added to the calcium hydroxide suspension.
A gas of 4-8 % by volume of CO2 in air was then bubbled upwards through the suspension at a rate of 100 m3/h under a suspension agitation of 200 to 300 rpm during 15 minutes, calculated from start of introduction of said gas. Thereafter, the CO2 volume fraction in the gas was augmented to 20-30 % under the same conditions until the end of the carbonation. Overpressure in gas feed was 100-150 mbar, corresponding to hydrostatic pressure of Ca(OH)2 suspension in the reactor.
When the C02-content in the exhaust gas exceeded 6 % by volume, hot dilution water, in an amount listed in Table 1, was added continuously into the reactor to obtain the viscosity listed in Table 1.
During carbonation, the temperature of the suspension was not controlled and allowed to rise due to the heat generated in the exothermic precipitation reaction.
After conductivity reached a minimum, gassing was continued for another 4 minutes and then stopped. The final product had a residual time content of less than 6 %
by weight relative to the weight of the final PCC product.
Figure 1A and Figure lB (enlargement of Figure 1A) show an SEM image of the obtained product of Test 9, featuring the typical needle shape of the aragonitic PCC
polymorph.
Carbonation time, representing the time elapsed between the start of gas introduction and reaching a conductivity minimum, and other product and process conditions, are given in Table 1.
Test 10 (Process according to the invention for the production of aragonitic PCC) This test was run under the same conditions as Test 9, according to the conditions listed in Table 1, with the addition of Polymer P to the calcium hydroxide suspension prior to commencing carbonation, in an amount listed in Table 1.
Figure 2A and Figure 2B (enlargement of Figure 2A) show an SEM image of the obtained product of Test 10, featuring the typical needle shape of the aragonitic PCC
polymorph.
The final PCC product had a residual lime content of less than 6 % by weight.
Other results are given in Table 1.
Test 11 (Prior art process for the production of aragonitic PCC) This test was run under the same conditions as Test 9, according to the conditions listed in Table 1, with the addition of PEG to the calcium hydroxide suspension prior to commencing carbonation, in an amount listed in Table 1.
Results are given in Table 1.
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=CJ ti r` I-- NN N N N NN N
r r r r r r r r r r r O Qv N S_ >OUV) C N o N 00 P)) co N 0) IR (Q T7 CO CM M N M N CO N C M M
.N \ r r r r r r r r r r 00 v)3 c a) O to (L) U) IC) 0 O a) O O
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O) 07 0 0 O O O O O O
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c O. a cL c a. d a- a. a_ a. a- a_ (L 0-~- N m d' U) (0 r` CO 0) O r ti N r r O
H
In the above Table, the reference "S-PCC" indicates a PCC of essentially scalenohedral polymorph, as determined according to an SEM image of the product. The reference "A-PCC" refers to an essentially aragonitic PCC product according to SEM images.
5 The results of Table 1 clearly demonstrate that only the process according to the present invention leads to a high PCC production rate relative to the carbonation time and final PCC suspension weight, without compromising the nature of the PCC polymorph or other PCC characteristics, relative to the same process run in absence of the polymer according to the invention.
Following the obtention of the PCC-comprising suspension in step (iv), he may wish to concentrate this suspension by mechanical and/or thermal concentration. During such a concentration, it may be advantageous to add dispersing additives, such as common polyacrylates.
It is of note that should additional polymer according to the present invention be implemented as a dispersant during steps (v) and (vi), less must be added than when concentrating a PCC-comprising suspension not obtained by the present invention.
Said PCC of step (iv) may also be dried.
Product-by-process The present invention also lies in the aqueous suspension from the inventive process.
The present invention also lies in a dry product obtained by drying the aqueous suspension from the inventive process.
As regards this dry product, it generally features the same or less residual calcium hydroxide as a product obtained by the same process but in the absence of said polymer, the residual lime content being determined by XRD analysis. Indeed, it is among the advantages of the present invention that the degree of conversion of calcium hydroxide to PCC is not negatively affected.
Moreover, this dry product may contain less than 6 %, and preferably less than 3 %, by weight relative to the weight of the total product weight, of residual calcium hydroxide.
Use of the product-by-process The PCC-comprising suspension or dry product obtained following the process of the 5 present invention finds applications in paper, paint or plastic, and especially in paper or plastic.
EXAMPLES
Example 1 In the Tests below, PCC was synthesised by bubbling a C02-comprising gas through a suspension of calcium hydroxide.
Additives according to the prior art and according to the process of the invention were implemented. The following prior art additives were used:
- PAA is a sodium polyacrylate with a molecular weight of about 10 500 g/mol - PEG is a polyethylene glycol with a molecular weight of about 600 g/mol The following additive according to the process of the invention was used:
- Polymer P is a polymer resulting from the polymerisation of the following monomers (expressed in % monomer units of each constituent):
- monomer a) 79,8 % of methacrylic acid and 9,0 % of ethyl acrylate - monomer b) 11,2 % of a monomer featuring a vinyl group on which:
- a first substituent consists of Formula (I), wherein:
R = ester function;
R' = methyl group;
m = 0;
p0;
n = 45;
q= 1;
- a second substituent consists of a methyl group;
- the first and second substituents above are in trans-position relative to one another.
The efficiency of the PCC production process was determined according to the weight of PCC produced (in kg) relative to both carbonation time (in hours) and final PCC
suspension weight (in kg).
The obtained precipitated calcium carbonate polymorph was determined by visual analysis of the SEM images of the product.
The particle size characteristics of the obtained PCC (median diameter (dso), where the value dx represents the diameter relative to which X % by weight of the particles have a diameter less than dx) was determined based on measurements made using SedigraphTM
5100 instrumentation from MICROMERITICSTM.
The specific surface area (in m2/g) of the obtained PCC was determined using the BET
method, according to ISO 9277:1995.
The BrookfieldTM viscosity of the final PCC suspension was measured at 25 C
under 100 rpm ( i2).
Residual lime content in the obtained PCC was determined by XRD analysis.
Test 1 (Reference process for the production of scalenohedral PCC) 200 kg of calcium oxide (origin: Austria) were added to 1 700 litres of 40 C-tap water in a stirred reactor; the reactor contents were mixed under continuous stirring for 30 minutes. The resulting suspension of calcium hydroxide was diluted with water to obtain a suspension featuring a dry weight of calcium hydroxide as listed in Table 1.
1 750 litres of this calcium hydroxide suspension was then brought to a temperature of 50 C and directed into a 1 800 litre cylindrical stainless steel reactor equipped with an agitator and probes monitoring the pH and conductivity of the suspension.
A gas of 20-30 % by volume of CO2 in air was then bubbled upwards through the suspension at a rate of 200 m3/h under a suspension agitation of between 200 and 300 rpm. Overpressure in gas feed was 150-200 mbar, corresponding to hydrostatic pressure of Ca(OH)2 suspension in the reactor.
During carbonation, the temperature of the suspension was not controlled and allowed to rise due to the heat generated in the exothermic precipitation reaction.
After conductivity reached a minimum, gassing was continued for another 4 minutes and then stopped. The final product had a residual lime content of less than 6 %
by weight relative to the weight of the final PCC product.
Carbonation time, representing the time elapsed between the start of gas introduction and reaching a conductivity minimum, and other product and process conditions, are given in Table 1.
Test 2 (Prior art process for the production of scalenohedral PCC) This test was run under the same conditions as Test 1, according to the conditions listed in Table 1, with the addition of PAA to the Ca(OH)2 suspension prior to carbonation in an amount listed in Table 1.
Results are given in Table 1.
Test 3 (Process according to the invention for the production of scalenohedral PCC) This test was run under the same conditions as Test 1, according to the conditions listed in Table 1, with the addition of Polymer P to the Ca(OH)2 suspension prior to carbonation in an amount listed in Table 1.
The final PCC product had a residual lime content of less than 6 % by weight.
Other results are given in Table 1.
Test 4 (Reference process for the production of aragonitic PCC) 160 kg of calcium oxide (origin: USA) were added to 1 300 litres of 50 C-tap water in a stirred reactor; the reactor contents were mixed under continuous stirring for 30 minutes.
The resulting suspension of calcium hydroxide was diluted with water to obtain a suspension featuring a dry weight of calcium hydroxide as listed in Table 1.
1 250 litres of this calcium hydroxide suspension was then brought to a temperature of 60 C and directed into a 1 800 litre cylindrical stainless steel reactor equipped with an agitator and probes monitoring the pH and conductivity of the suspension as well as the CO2 content of the exhaust gas.
Before start of carbonation, aragonite structure-promoting seed was added to the calcium hydroxide suspension.
A gas of 4-8 % by volume of CO2 in air was then bubbled upwards through the suspension at a rate of 100 m3/h under a suspension agitation of 200 to 300 rpm during 15 minutes, calculated from start of introduction of said gas. Thereafter, the CO2 volume fraction in the gas was augmented to 20-30 % under the same conditions until the end of the carbonation. Overpressure in gas feed was 100-150 mbar, corresponding to hydrostatic pressure of Ca(OH)2 suspension in the reactor.
When the C02-content in the exhaust gas exceeded 6 % by volume, hot dilution water, in an amount listed in Table 1, was added continuously into the reactor to obtain the viscosity listed in Table 1.
During carbonation, the temperature of the suspension was not controlled and allowed to rise due to the heat generated in the exothermic precipitation reaction.
After conductivity reached a minimum, gassing was continued for another 4 minutes and then stopped. The final product had a residual lime content of less than 6 %
by weight relative to the weight of the final PCC product.
5 Carbonation time, representing the time elapsed between the start of gas introduction and reaching a conductivity minimum, and other product and process conditions are given in Table 1.
Test 5 (Process according to the invention for the production of aragonitic PCC) This test was run under the same conditions as Test 4, according to the conditions listed in Table 1, with the addition of Polymer P to the water subsequently added to calcium oxide to form the calcium hydroxide suspension, in an amount listed in Table 1.
The final PCC product had a residual lime content of less than 6 % by weight.
Other results are given in Table 1.
Test 6 (Process according to the invention for the production of aragonitic PCC) This test was run under the same conditions as Test 4, according to the conditions listed in Table 1, with the addition of Polymer P to the calcium hydroxide suspension prior to commencing carbonation, in an amount listed in Table 1.
The final PCC product had a residual lime content of less than 6 % by weight.
Other results are given in Table 1.
Test 7 (Process according to the invention for the production of aragonitic PCC) This test was run under the same conditions as Test 4, according to the conditions listed in Table 1, with the addition of Polymer P to the calcium hydroxide suspension prior to commencing carbonation, in an amount listed in Table 1.
The final PCC product had a residual lime content of less than 6 % by weight.
Other results are given in Table 1.
Test 8 (Process according to the invention for the production of aragonitic PCC) This test was run under the same conditions as Test 4, according to the conditions listed in Table 1, with the addition of Polymer P to the calcium hydroxide suspension prior to commencing carbonation, in an amount listed in Table 1.
The final PCC product had a residual lime content of less than 6 % by weight.
Other results are given in Table 1.
Test 9 (Reference process for the production of aragonitic PCC) 160 kg of calcium oxide (origin: Austria) were added to 1 300 litres of 50 C-tap water in a stirred reactor; the reactor contents were mixed under continuous stirring for 30 minutes. The resulting suspension of calcium hydroxide was diluted with water to obtain a suspension featuring a dry weight of calcium hydroxide as listed in Table 1.
1 250 litres of this calcium hydroxide suspension was then brought to a temperature of 60 C and directed into a 1 800 litre cylindrical stainless steel reactor equipped with an agitator and probes monitoring the pH and conductivity of the suspension as well as the CO2 content of the exhaust gas.
Before the start of carbonation, aragonite structure-promoting seed was added to the calcium hydroxide suspension.
A gas of 4-8 % by volume of CO2 in air was then bubbled upwards through the suspension at a rate of 100 m3/h under a suspension agitation of 200 to 300 rpm during 15 minutes, calculated from start of introduction of said gas. Thereafter, the CO2 volume fraction in the gas was augmented to 20-30 % under the same conditions until the end of the carbonation. Overpressure in gas feed was 100-150 mbar, corresponding to hydrostatic pressure of Ca(OH)2 suspension in the reactor.
When the C02-content in the exhaust gas exceeded 6 % by volume, hot dilution water, in an amount listed in Table 1, was added continuously into the reactor to obtain the viscosity listed in Table 1.
During carbonation, the temperature of the suspension was not controlled and allowed to rise due to the heat generated in the exothermic precipitation reaction.
After conductivity reached a minimum, gassing was continued for another 4 minutes and then stopped. The final product had a residual time content of less than 6 %
by weight relative to the weight of the final PCC product.
Figure 1A and Figure lB (enlargement of Figure 1A) show an SEM image of the obtained product of Test 9, featuring the typical needle shape of the aragonitic PCC
polymorph.
Carbonation time, representing the time elapsed between the start of gas introduction and reaching a conductivity minimum, and other product and process conditions, are given in Table 1.
Test 10 (Process according to the invention for the production of aragonitic PCC) This test was run under the same conditions as Test 9, according to the conditions listed in Table 1, with the addition of Polymer P to the calcium hydroxide suspension prior to commencing carbonation, in an amount listed in Table 1.
Figure 2A and Figure 2B (enlargement of Figure 2A) show an SEM image of the obtained product of Test 10, featuring the typical needle shape of the aragonitic PCC
polymorph.
The final PCC product had a residual lime content of less than 6 % by weight.
Other results are given in Table 1.
Test 11 (Prior art process for the production of aragonitic PCC) This test was run under the same conditions as Test 9, according to the conditions listed in Table 1, with the addition of PEG to the calcium hydroxide suspension prior to commencing carbonation, in an amount listed in Table 1.
Results are given in Table 1.
d' r to 00 M U) 'd' C) CO CO
¾ LO O 00 O) 00 Co (A 00 0) U) W
U) In C0 N In co 0 O r CO r L) co co E CO N d OR CO 0) O) U) Ci) 0) -~ c' CV N r r r r r r r r U~o UUU UU U U 0 0 0 0 a 0 a 0_ a. a. a. a. al a a_ DoE cnv)~ Qd Q Q Q ¾¾ Q
LO co N- d CO CO (0 - to CO
U C r r r r r r r r r r r CI) N 4 V5 C) C) O 0 0 O O O C) 0 O
Lam'3Q:._, >_ a) 't3 p N o O U va) U c It O N ml- d U) C O N CO
O ti cm U) r CO N CO N O) LO
to N 00 In <t r m d Yv-0.. cn w CO 00 u) CD Cl O 0) LO Co In 00 O
70 N r r N 0 0) to N 04 N N
y (D CO N N
c= o .) E a) CL > Cn .~ L _ 'N a) a) a) 0 0 0 a) a) 0 0 0 c C c In In O c c In LO LO
~~ _ ' y J C c c CO CO - 0 0 Q . 0 'C) D m c > ..+
r ti r O co O CO r N 0 In Q) CO N CO CO CO CO CO CO ~t r CO
m CO Co N N N N N N N N
a) (D
C l)0 2 H~aa~
LO N In O CO O to 0) O d' it' 'd' ti ti I` I` ti ti 00 N.
N N N r r r r r r r r LO It 4d, IC) 0) d' N CO C0 IC) IT
C N c CO N- to (0 LO In Co CO C0 CO co N o a E
IC) In U) In U) In I) In LO U) LO
=CJ ti r` I-- NN N N N NN N
r r r r r r r r r r r O Qv N S_ >OUV) C N o N 00 P)) co N 0) IR (Q T7 CO CM M N M N CO N C M M
.N \ r r r r r r r r r r 00 v)3 c a) O to (L) U) IC) 0 O a) O O
C O N- C ti In C) C O 0 > 'C h 0 r 0 0 o 0 r N 0 r r '= N 2' ~,..C O C C C
O) 07 0 0 O O O O O O
> a) C E C T ?. 5+ E C >1 CD
'a 0 0 0 0 0 0 0 0 0 W
c O. a cL c a. d a- a. a_ a. a- a_ (L 0-~- N m d' U) (0 r` CO 0) O r ti N r r O
H
In the above Table, the reference "S-PCC" indicates a PCC of essentially scalenohedral polymorph, as determined according to an SEM image of the product. The reference "A-PCC" refers to an essentially aragonitic PCC product according to SEM images.
5 The results of Table 1 clearly demonstrate that only the process according to the present invention leads to a high PCC production rate relative to the carbonation time and final PCC suspension weight, without compromising the nature of the PCC polymorph or other PCC characteristics, relative to the same process run in absence of the polymer according to the invention.
Claims (63)
1. Process for preparing a precipitated calcium carbonate, PCC, said process comprising the following steps:
providing CaO, as a calcium source;
(ii) providing a CO2-comprising gas;
(iii) contacting said calcium source of step (i) and said CO2-comprising gas of step (ii) in an aqueous environment in a reactor, in one or more steps;
(iv) obtaining a PCC-comprising suspension;
characterised in that:
- is present during step (iii) at least one polymer resulting from the polymerisation of the following monomers, where such monomers are present in said polymer in the following % monomer units relative to the total monomer units forming said polymer:
a) from 10 % to 99 % of at least one vinyl group-comprising monomer which is distinct from the monomer comprising formula (I), b) from 1 % to 90 % of at least one vinyl group-comprising monomer having at least one substituent comprising formula (I) :
wherein :
- m, n, p and q are whole numbers having a value of less than 150, and at least one of m, n, p and q has a value of greater than 0, such that 25 <
(m+n+p)q < 150;
- R represents a functional linking group selected from the group consisting of ethers, esters and amides, - R1 and R2 are the same or different, and represent hydrogen or alkyl groups having 1 to 4 carbon atoms, - R' represents hydrogen or a hydrocarbon radical having 1 to 40 carbon atoms, the sum of the monomer unit percentages of monomers a) and b) being equal to 100 %.
providing CaO, as a calcium source;
(ii) providing a CO2-comprising gas;
(iii) contacting said calcium source of step (i) and said CO2-comprising gas of step (ii) in an aqueous environment in a reactor, in one or more steps;
(iv) obtaining a PCC-comprising suspension;
characterised in that:
- is present during step (iii) at least one polymer resulting from the polymerisation of the following monomers, where such monomers are present in said polymer in the following % monomer units relative to the total monomer units forming said polymer:
a) from 10 % to 99 % of at least one vinyl group-comprising monomer which is distinct from the monomer comprising formula (I), b) from 1 % to 90 % of at least one vinyl group-comprising monomer having at least one substituent comprising formula (I) :
wherein :
- m, n, p and q are whole numbers having a value of less than 150, and at least one of m, n, p and q has a value of greater than 0, such that 25 <
(m+n+p)q < 150;
- R represents a functional linking group selected from the group consisting of ethers, esters and amides, - R1 and R2 are the same or different, and represent hydrogen or alkyl groups having 1 to 4 carbon atoms, - R' represents hydrogen or a hydrocarbon radical having 1 to 40 carbon atoms, the sum of the monomer unit percentages of monomers a) and b) being equal to 100 %.
2. The process according to claim 1, characterized in that said process further comprises the following step:
(v) concentrating said PCC-comprising suspension of step (iv).
(v) concentrating said PCC-comprising suspension of step (iv).
3. The process according to claim 1, characterized in that said process further comprises the following step:
(iv) adding dispersing additives to the suspension of step (iv).
(iv) adding dispersing additives to the suspension of step (iv).
4. The process according to claim 1, characterized in that said process further comprises the following steps:
(v) concentrating said PCC-comprising suspension of step (iv); and (iv) adding dispersing additives to the suspension of step (iv) and/or (v).
(v) concentrating said PCC-comprising suspension of step (iv); and (iv) adding dispersing additives to the suspension of step (iv) and/or (v).
5. The process according to any one of claims 1 to 4, characterized in that during step (iii) the monomers are present in said polymer in the following % monomer units relative to the total monomer units forming said polymer, is present during step (iii):
a) from 50 % to 98 % of at least one vinyl group-comprising monomer distinct from the monomer comprising formula (l), b) from 2 % to 50 % of at least one vinyl group-comprising monomer having at least one substituent comprising formula (l).
a) from 50 % to 98 % of at least one vinyl group-comprising monomer distinct from the monomer comprising formula (l), b) from 2 % to 50 % of at least one vinyl group-comprising monomer having at least one substituent comprising formula (l).
6. The process according to any one of claims 1 to 4, characterized in that during step (iii) the monomers are present in said polymer in the following % monomer units relative to the total monomer units forming said polymer, is present during step (iii):
a) from 80 % to 97 % of at least one vinyl group-comprising monomer distinct from the monomer comprising formula (l), b) from 3 % to 20 %of at least one vinyl group-comprising monomer having at least one substituent comprising formula (l).
a) from 80 % to 97 % of at least one vinyl group-comprising monomer distinct from the monomer comprising formula (l), b) from 3 % to 20 %of at least one vinyl group-comprising monomer having at least one substituent comprising formula (l).
7. The process according to any one of claims 1 to 4, characterized in that during step (iii) the monomers are present in said polymer in the following % monomer units relative to the total monomer units forming said polymer, a) from 85 % to 95 % of at least one vinyl group-comprising monomer distinct from the monomer comprising formula (l), b) from 5 % to 15 % of at least one vinyl group-comprising monomer having at least one substituent comprising formula (l).
8. The process according to any one of claims 1 to 7, characterized in that 50 <=
(m+n+.rho.)q < 150.
(m+n+.rho.)q < 150.
9. The process according to any one of claims 1 to 8, characterized in that R' represents hydrogen or a hydrocarbon radical having 1 to 3 carbon atoms.
10. The process according to any one of claims 1 to 9, characterized in that R' represents a methyl radical or hydrogen.
11. The process according to any one of claims 1 to 10, characterised in that said monomer(s) (a) are selected from the group consisting of anionic monomers, cationic monomers, neutral monomers and mixtures thereof.
12. The process according to claim 11, characterised in that the anionic monomers are selected from the group consisting of monomers of acrylic acid, methacrylic acid and maleic acid, the cationic monomers are selected from the group consisting of acrylamide and methacrylamide, and neutral monomers are selected from the group consisting of acrylic acid esters, methacrylic acid esters and maleic acid esters.
13. The process according to claim 11 or 12, characterised in that said monomer(s) (a) are a mixture of anionic and neutral monomer(s).
14. The process according to claim 13, characterised in that the monomer unit ratio of anionic monomers:neutral monomers is from 50:50 to 2:1.
15. The process according to claim 13, characterised in that the monomer unit ratio of anionic monomers:neutral monomers is from 8:1 to 12:1.
16. The process according to claim 13, characterised in that the monomer unit ratio of anionic monomers:neutral monomers is from 10 : 1.
17. The process according to any one of claims 13 to 16, characterised in that said monomer(s) (a) are a mixture of anionic and neutral monomer(s) selected from the group consisting of acrylic acid, methacrylic acid, acrylic acid esters and methacrylic acid esters.
18. The process according to claim 12 or 13, characterised in that said cationic monomer(s) are selected from the group consisting of cationic (meth)acrylic esters.
19. The process according to claim 18, characterised in that said cationic monomer(s) are selected from the group consisting of chloride salts of [2-(methacryloyloxy)ethyl]trimethyl ammonium, [3-acrylamido)propyl]trimethylammonium, dimethyl diallyl ammonium and [3-(methacrylamido)propyl]trimethylammonium, sulfate salts of [2-(methacryloyloxy)ethyl]trimethyl ammonium, [3-acrylamido)propyl]trimethylammonium, dimethyl diallyl ammonium and [3-(methacrylamido)propyl]trimethylammonium, and mixture thereof.
20. The process according to any one of claims 1 to 19, characterised in that said monomer(s) (b) additionally comprise one or more substituents distinct from the monomer comprising the formula (l) and represent functional groups selected from the group consisting of alkyl, aryl, alkyl ester, hydrogen, alkyl amide, carboxyl and allyl.
21. The process according to claim 20, characterised in that said one or more substituents comprise at least one methyl substituent.
22. The process according to claim 20 or 21, characterised in that said monomer(s) (b) comprise a methyl group in trans-position relative to said substituent comprising formula (l) in which said functional group linking is an ester.
23. The process according to any one of claims 1 to 22, characterised in that said monomer(s) (b) have at least one substituent consisting of formula (l).
24. The process according to any one of claims 1 to 23, characterised in that said polymer is added in an amount totalling 0.01 % to 0.5 % by dry weight relative to the dry weight of PCC obtained in step (iv).
25. The process according to claim 24, characterised in that said polymer is added in an amount totalling 0.05 % to 0.2% by dry weight relative to the dry weight of PCC
obtained in step (iv).
obtained in step (iv).
26. The process according to any one of claims 1 to 25, characterised in that said polymer has an intrinsic viscosity of less than or equal to 100 ml/g.
27. The process according to any one of claims 1 to 26, characterised in that said polymer is fractionated in doses added over time prior to and/or during step (iii).
28. The process according to any one of claims 1 to 27, characterised in that said polymer is added during more than one of steps (i), (ii) and (iii).
29. The process according to any one of claims 1 to 28, characterised in that 20 %
by weight of the polymer is added prior to reaching an aqueous environment maximum viscosity during step (iii).
by weight of the polymer is added prior to reaching an aqueous environment maximum viscosity during step (iii).
30. The process according to claim 29, characterised in that 50 % by weight of the polymer is added prior to reaching an aqueous environment maximum viscosity during step (iii).
31. The process according to claim 29, characterised in that 80 % by weight of the polymer is added prior to reaching an aqueous environment maximum viscosity during step (iii).
32. The process according to claim 29, characterised in that 100 % by weight of the polymer is added prior to reaching an aqueous environment maximum viscosity during step (iii).
33. The process according to any one of claims 1 to 29, characterised in that 20 %
by weight of the polymer is added prior to reaching an aqueous environment conductivity drop associated with a conductivity curve inflection point slope of more than 45° during step (iii).
by weight of the polymer is added prior to reaching an aqueous environment conductivity drop associated with a conductivity curve inflection point slope of more than 45° during step (iii).
34. The process according to any one of claims 1 to 28 and 30, characterised in that 50 % by weight of the polymer is added prior to reaching an aqueous environment conductivity drop associated with a conductivity curve inflection point slope of more than 45° during step (iii).
35. The process according to any one of claims 1 to 28 and 31, characterised in that 80 % by weight of the polymer is added prior to reaching an aqueous environment conductivity drop associated with a conductivity curve inflection point slope of more than 45° during step (iii).
36. The process according to any one of claims 1 to 28 and 32, characterised in that 100 % by weight of the polymer is added prior to reaching an aqueous environment conductivity drop associated with a conductivity curve inflection point slope of more than 45° during step (iii).
37. The process according to any one of claims 1 to 29 and 33, characterised in that 20 % by weight of the polymer is added prior to reaching a pH value of less than 7.2 during step (iii).
38. The process according to any one of claims 1 to 28, 30 and 34, characterised in that 50 % by weight of the polymer is added prior to reaching a pH value of less than 7.2 during step (iii).
39. The process according to any one of claims 1 to 28, 31 and 35, characterised in that 80 % by weight of the polymer is added prior to reaching a pH value of less than 7.2 during step (iii).
40. The process according to any one of claims 1 to 28, 32 and 36, characterised in that 100 % by weight of the polymer is added prior to reaching a pH value of less than 7.2 during step (iii).
41. The process according to any one of claims 1 to 29, 33 and 37, characterised in that 20 % by weight of the polymer is added prior to step (iii).
42. The process according to any one of claims 1 to 28, 30, 34 and 38, characterised in that 50 % by weight of the polymer is added prior to step (iii).
43. The process according to any one of claims 1 to 28, 31, 35 and 39, characterised in that 80 % by weight of the polymer is added prior to step (iii).
44. The process according to any one of claims 1 to 28, 32, 36 and 40, characterised in that 100 % by weight of the polymer is added prior to step (iii).
45. The process according to any one of claims 1 to 44, characterised in that said CaO of step (i) is partially or fully slaked by addition of slaking water to form a slaked lime suspension prior to step (iii).
46. The process according to any one of claims 1 to 29, 33, 37 and 41, characterised in that said CaO of step (i) is partially or fully slaked by addition of slaking water to form a slaked lime suspension prior to step (iii) and characterised in that 20 %
by weight of the polymer is added to said slaking water.
by weight of the polymer is added to said slaking water.
47. The process according to any one of claims 1 to 28, 30, 34, 38 and 42, characterised in that said CaO of step (i) is partially or fully slaked by addition of slaking water to form a slaked lime suspension prior to step (iii) and characterised in that 50 %
by weight of the polymer is added to said slaking water.
by weight of the polymer is added to said slaking water.
48. The process according to any one of claims 1 to 28, 31, 35, 39 and 43, characterised in that said CaO of step (i) is partially or fully slaked by addition of slaking water to form a slaked lime suspension prior to step (iii) and characterised in that 80 %
by weight of the polymer is added to said slaking water.
by weight of the polymer is added to said slaking water.
49. The process according to any one of claims 1 to 28, 32, 36, 40 and 44, characterised in that said CaO of step (i) is partially or fully slaked by addition of slaking water to form a slaked lime suspension prior to step (iii) and characterised in that 100 %
by weight of the polymer is added to said slaking water.
by weight of the polymer is added to said slaking water.
50. The process according to any one of claims 1 to 29, 33, 37 and 41, characterised in that said CaO of step (i) is partially or fully slaked by addition of slaking water to form a slaked lime suspension prior to step (iii) and characterised in that 20 %
by weight of the polymer is added to said slaked lime suspension prior to step (iii).
by weight of the polymer is added to said slaked lime suspension prior to step (iii).
51. The process according to any one of claims 1 to 28, 30, 34, 38 and 42, characterised in that said CaO of step (i) is partially or fully slaked by addition of slaking water to form a slaked lime suspension prior to step (iii) and characterised in that 50 %
by weight of the polymer is added to said slaked lime suspension prior to step (iii).
by weight of the polymer is added to said slaked lime suspension prior to step (iii).
52. The process according to any one of claims 1 to 28, 31, 35, 39 and 43, characterised in that said CaO of step (i) is partially or fully slaked by addition of slaking water to form a slaked lime suspension prior to step (iii) and characterised in that 80 %
by weight of the polymer is added to said slaked lime suspension prior to step (iii).
by weight of the polymer is added to said slaked lime suspension prior to step (iii).
53. The process according to any one of claims 1 to 28, 32, 36, 40 and 44, characterised in that said CaO of step (i) is partially or fully slaked by addition of slaking water to form a slaked lime suspension prior to step (iii) and characterised in that 100 %
by weight of the polymer is added to said slaked lime suspension prior to step (iii).
by weight of the polymer is added to said slaked lime suspension prior to step (iii).
54. The process according to any one of claims 1 to 53, characterised in that the step of contacting of the calcium source of step (i) and the CO2-comprising gas of step (ii) is carried out in the reactor by bubbling the CO2-comprising gas in the aqueous environment, said bubbling being performed until the conductivity of the aqueous environment drops.
55. The process according to claim 54, characterised in that said bubbling is performed until an aqueous environment pH of 7.5 is reached.
56. The process according to claim 55, characterised in that said bubbling is performed until an aqueous environment pH of 7.2 is reached.
57. The process according to any one of claims 1 to 56, characterised in that said CO2-comprising gas is provided at an overpressure of at least 0.1 bar relative to the pressure in said reactor.
58. The process according to claim 57, characterised in that said CO2-comprising gas is provided at an overpressure of at least 0.2 bar relative to the pressure in said reactor.
59. The process according to claim 57, characterised in that said CO2-comprising gas is provided at an overpressure of at least 0.3 bar relative to the pressure in said reactor.
60. The process according to claim 57, characterised in that said CO2-comprising gas is provided at an overpressure of at least 0.4 bar relative to the pressure in said reactor.
61. The process according to claim 57, characterised in that said CO2-comprising gas is provided at an overpressure of at least 0.6 bar relative to the pressure in said reactor.
62. The process according to any one of claims 1 to 61, characterised in that the PCC-comprising suspension of step (iv) is concentrated by mechanical and/or thermal concentration.
63. The process according to any one of claims 1 to 62, characterised in that said PCC of step (iv) is dried.
Applications Claiming Priority (5)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| EP08014443.9A EP2157136B1 (en) | 2008-08-13 | 2008-08-13 | Precipitated calcium carbonate obtained by a process implementing low charge acrylate and/or maleinate containing polymer |
| EP08014443.9 | 2008-08-13 | ||
| US10031908P | 2008-09-26 | 2008-09-26 | |
| US61/100,319 | 2008-09-26 | ||
| PCT/IB2009/006431 WO2010018432A1 (en) | 2008-08-13 | 2009-08-04 | Process to prepare precipitated calcium carbonate implementing low charge acrylate a/o maleinate -containing polymer |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CA2733080A1 CA2733080A1 (en) | 2010-02-18 |
| CA2733080C true CA2733080C (en) | 2017-05-16 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA2733080A Expired - Fee Related CA2733080C (en) | 2008-08-13 | 2009-08-04 | Process to prepare precipitated calcium carbonate implementing low charge acrylate a/o maleinate-containing polymer |
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| Country | Link |
|---|---|
| US (1) | US9017631B2 (en) |
| EP (2) | EP2157136B1 (en) |
| KR (1) | KR101724160B1 (en) |
| CN (1) | CN102124061B (en) |
| BR (1) | BRPI0918000A2 (en) |
| CA (1) | CA2733080C (en) |
| DK (1) | DK2318464T3 (en) |
| ES (1) | ES2609310T3 (en) |
| HR (1) | HRP20161633T1 (en) |
| MX (1) | MX343447B (en) |
| PL (1) | PL2318464T3 (en) |
| PT (2) | PT2157136T (en) |
| RU (1) | RU2509788C2 (en) |
| SI (1) | SI2318464T1 (en) |
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| WO (1) | WO2010018432A1 (en) |
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| FR2907347B1 (en) * | 2006-10-19 | 2008-12-05 | Coatex Sas | USE OF A STERIC DISPERSIENT AGENT OF MINERAL MATERIALS IN WATER, AQUEOUS DISPERSION OBTAINED AND USE THEREOF IN THE MANUFACTURE OF PAPER |
| FR2911147B1 (en) | 2007-01-09 | 2009-02-13 | Coatex S A S Soc Par Actions S | PROCESS FOR THE MANUFACTURE OF AN OXIDE POWDER AND METAL HYDROXIDE AUTODISPERSABLE IN WATER, POWDER AND AQUEOUS DISPERSION OBTAINED, AND USES THEREOF |
| FR2934992B1 (en) * | 2008-08-13 | 2010-08-27 | Coatex Sas | USE OF A LOW IONIC ACRYLIC POLYMER IN THE SYNTHESIS OF PRECIPITATED CALCIUM CARBONATE |
-
2008
- 2008-08-13 EP EP08014443.9A patent/EP2157136B1/en active Active
- 2008-08-13 PT PT08014443T patent/PT2157136T/en unknown
-
2009
- 2009-08-04 CN CN200980131263.3A patent/CN102124061B/en not_active Expired - Fee Related
- 2009-08-04 EP EP09786092.8A patent/EP2318464B1/en active Active
- 2009-08-04 CA CA2733080A patent/CA2733080C/en not_active Expired - Fee Related
- 2009-08-04 KR KR1020117004226A patent/KR101724160B1/en active IP Right Grant
- 2009-08-04 PT PT97860928T patent/PT2318464T/en unknown
- 2009-08-04 RU RU2011109185/05A patent/RU2509788C2/en not_active IP Right Cessation
- 2009-08-04 DK DK09786092.8T patent/DK2318464T3/en active
- 2009-08-04 BR BRPI0918000A patent/BRPI0918000A2/en not_active Application Discontinuation
- 2009-08-04 US US12/737,595 patent/US9017631B2/en active Active
- 2009-08-04 MX MX2011001505A patent/MX343447B/en active IP Right Grant
- 2009-08-04 ES ES09786092.8T patent/ES2609310T3/en active Active
- 2009-08-04 WO PCT/IB2009/006431 patent/WO2010018432A1/en active Application Filing
- 2009-08-04 SI SI200931568A patent/SI2318464T1/en unknown
- 2009-08-04 PL PL09786092T patent/PL2318464T3/en unknown
- 2009-08-05 TW TW098126338A patent/TW201012756A/en unknown
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2016
- 2016-12-05 HR HRP20161633TT patent/HRP20161633T1/en unknown
Also Published As
| Publication number | Publication date |
|---|---|
| CN102124061A (en) | 2011-07-13 |
| US20110158890A1 (en) | 2011-06-30 |
| RU2011109185A (en) | 2012-09-20 |
| CN102124061B (en) | 2014-04-23 |
| EP2157136A1 (en) | 2010-02-24 |
| EP2318464A1 (en) | 2011-05-11 |
| SI2318464T1 (en) | 2017-01-31 |
| HRP20161633T1 (en) | 2017-01-13 |
| PT2157136T (en) | 2019-06-21 |
| MX2011001505A (en) | 2011-04-26 |
| MX343447B (en) | 2016-11-07 |
| RU2509788C2 (en) | 2014-03-20 |
| DK2318464T3 (en) | 2017-01-16 |
| CA2733080A1 (en) | 2010-02-18 |
| EP2318464B1 (en) | 2016-09-28 |
| EP2157136B1 (en) | 2019-03-20 |
| WO2010018432A1 (en) | 2010-02-18 |
| US9017631B2 (en) | 2015-04-28 |
| PL2318464T3 (en) | 2017-04-28 |
| KR101724160B1 (en) | 2017-04-06 |
| PT2318464T (en) | 2016-12-15 |
| ES2609310T3 (en) | 2017-04-19 |
| BRPI0918000A2 (en) | 2015-11-17 |
| KR20110058779A (en) | 2011-06-01 |
| TW201012756A (en) | 2010-04-01 |
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